WO2011038089A1 - Procédé de séchage du charbon - Google Patents

Procédé de séchage du charbon Download PDF

Info

Publication number
WO2011038089A1
WO2011038089A1 PCT/US2010/049957 US2010049957W WO2011038089A1 WO 2011038089 A1 WO2011038089 A1 WO 2011038089A1 US 2010049957 W US2010049957 W US 2010049957W WO 2011038089 A1 WO2011038089 A1 WO 2011038089A1
Authority
WO
WIPO (PCT)
Prior art keywords
coal
fluidized bed
bed reactor
water
temperature
Prior art date
Application number
PCT/US2010/049957
Other languages
English (en)
Inventor
David D. Dunlop
Clinton B. Camper
Vijay Sethi
Leon C. Kenyon, Jr.
Original Assignee
River Basin Energy, Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by River Basin Energy, Inc. filed Critical River Basin Energy, Inc.
Priority to AU2010298284A priority Critical patent/AU2010298284B2/en
Priority to CA2780314A priority patent/CA2780314A1/fr
Priority to EP10819441.6A priority patent/EP2480641A4/fr
Publication of WO2011038089A1 publication Critical patent/WO2011038089A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means
    • C10L9/06—Treating solid fuels to improve their combustion by chemical means by oxidation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
    • F26B3/084—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed with heat exchange taking place in the fluidised bed, e.g. combined direct and indirect heat exchange
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • a multi-stage process for drying coal in a fluidized bed reactor is provided.
  • a process for drying and reducing the equilibrium moisture of coal in a fluidized bed reactor is provided. More specifically, the process of one embodiment includes cooling the coal product from the fluidized bed reactor and adding moisture up to the reduced equilibrium moisture of the product to reduce the tendency of the product to self heat.
  • the '265 patent is illustrative of these patents that teaches a process for preparing an irreversibly dried coal with a first fluidized bed reactor that includes a first fluidized bed with a fluidized bed density of from about 30 to about 50 pounds per cubic foot is maintained at a temperature of from about 480 to about 600 degrees Fahrenheit. Coal with a moisture content of about 15 to about 30 percent and a particle size such that all of the coal particles in such coal are in the range of from 0 to 2 inches is fed into the first fluidized bed.
  • liquid phase water, inert gas, and air is fed into the first fluidized bed that is subjected, along with the coal, to a temperature of about 480 to about 600 degrees Fahrenheit for about 1 to about 5 minutes while simultaneously comminuting and dewatering said coal.
  • This process produces coal of coarse fraction and a fine fraction.
  • the fine fraction is sent to a cyclone wherein a portion of the fine fraction is removed and fed to a cooler that reduces the temperature of the fine fraction by at least about 300 degrees Fahrenheit.
  • the comminuted and dewatered coal is then passed to a second fluidized bed reactor that includes a second fluidized bed with a fluidized bed density of about 30 to about 50 pounds per cubic foot and a temperature of about 215 to about 250 degrees Fahrenheit.
  • Water, inert gas and oil of about 0.5 to about 3.0 weight percent of mineral oil having an initial boiling point of at least about 900 degrees Fahrenheit are also fed to the second fluidized bed.
  • the temperature change experienced by the coal as it moves from the first fluidized bed reactor to the second fluidized bed reactor, from about 480 to about 600 degrees Fahrenheit to about 215 to about 250 degrees Fahrenheit, and associated processes occur in less than about 120 seconds.
  • a multi-stage process for drying coal.
  • a coal with a moisture content of from about 15 to about 40 percent is heated in a first fluidized bed reactor at a temperature of between about 400 to about 650 degrees Fahrenheit until about 40 to about 60 percent of the water in such coal is removed and until at least about 50 percent of the particles less than about 400 microns are removed.
  • air is fed into the first fluidized bed reactor at a rate of from about 5 to about 8 feet per second.
  • the coal treated by the first fluidized bed reactor is heated in a second fluidized bed reactor at a temperature up to about 250 degrees Fahrenheit until the coal contains less than 1 weight percent of water.
  • the temperature used in the second fluidized bed reactor is at least about 50 degrees greater than the temperature used in the first fluidized bed reactor.
  • air is fed into the second fluidized bed reactor at a rate less than that associated with the first fluidized bed reactor.
  • pre-drying step that utilizes a fluidized bed reactor is contemplated, that other methods, may be employed to pre-dry the coal without departing from the scope of the invention. Furthermore, it will be appreciated that a pre-drying step may not be required.
  • one embodiment employs a fluid spray that cools the coal exiting the drying stage. The water also replaces at least a portion of the coals equilibrium moisture.
  • Fig. 1 is a schematic of one process for preparing a coal-water slurry
  • Fig. 2 is a schematic of one process for drying the coal used in the process of Fig. 1 ;
  • FIG. 3 is a schematic of one apparatus that may be used in the process of Fig. 2;
  • Fig. 4 is a schematic of another preferred apparatus that may be used in the process of Fig. 2;
  • Fig. 5 is a schematic of another embodiment of the present invention for cooling by immediately subjecting a product as it exits the fluid bed to a water spray of sufficient quantity to cool the blend and replace a portion of the blend equilibrium moisture;
  • Fig. 6 is a schematic of one process for drying coal
  • Fig. 7 is a detailed portion of Fig. 6;
  • Fig. 8 is a detailed portion of Fig. 6 showing a cooling portion.
  • a fluidized bed reactor is a system wherein a fluid or gas is passed through a granular solid material at high velocities to suspend the solid and cause it to behave as if it were fluid (i.e. fluidization).
  • the coal used in the process of this specification is similar to the coal having about 5 to about 30 weight percent of moisture and, more preferably about 10 to about 30 weight percent of moisture. However, in the instant case, the coal used may often contain up to about 40 weight percent of water.
  • the moisture content of coal may be determined by conventional means in accordance with standard A.S.T.M. testing procedures. Methods for determining the moisture content of coal are well known in the art; see, e.g., U.S. Pat. Nos. 5,527,365 (irreversible drying of carbonaceous fuels), 5,503,646, 5,41 1,560 (production of binderless pellets from low rank coal), 5,396,260, 5,361,513 (apparatus for drying and briquetting coal), 5, 21, 111, and the like. The entire disclosure of each of these United States patents is hereby incorporated by reference herein.
  • the coal used in the process of this invention contains from about 10 to about 25 percent of combined oxygen.
  • the coal used in the process of Fig. 1 contains from about 10 to about 20 weight of combined oxygen, in the form, e.g., of carboxyl groups, carbonyl groups, and hydroxyl groups.
  • combined oxygen means oxygen which is chemically bound to carbon atoms in the coal. See, e.g., H.H. Lowry, editor, “Chemistry of Coal Utilization” (John Wiley and Sons, Inc., New York, N.Y., 1963)....
  • the combined oxygen content of such coal may be determined, e.g., by standard analytical techniques; see, e.g., U.S. Patent Nos. 5,444,733, 5,171,474, 5,050,310, 4,852,384 (combined oxygen analyzer), 3,424,573, and the like.
  • standard analytical techniques see, e.g., U.S. Patent Nos. 5,444,733, 5,171,474, 5,050,310, 4,852,384 (combined oxygen analyzer), 3,424,573, and the like.
  • the disclosure of each of these United States patents is hereby incorporated by reference into this specification.
  • the coal used in the process of the instant invention contains about 10 to about 25 weight percent of ash. In one embodiment, the coal charged to feeder 12 contains at least about 10 weight percent of ash.
  • ash refers to the inorganic residue left after the ignition of combustible substances; see, e.g., U.S. Patent Nos. 5,534,137 (high ash coal), 5,521 ,132 (raw coal fly ash), 4,795,037 (high ash coal), 4,575,418 (removal of ash from coal), 4,486,894 (method and apparatus for sensing the ash content of coal), and the like. The disclosure of each of these United States patents is hereby incorporated by reference into this specification. By way of further illustration, one suitable ash containing coal which may be used in this embodiment is Herrin number 6 coal, from Illinois.
  • this coal is mixed with from about 25 to about 35 weight percent of water (by total weight of water and coal), the slurry thus produced is unstable. It is thus an object of one embodiment of this invention to provide a stable coal-water slurry made from subbituminous coal, wherein said slurry has a solids content of at least about 65 weight percent and a heating value that is at least about 80 percent of the heating value of the undried coal.
  • step 10 subbituminous coal is dried to a moisture content of less than about 5 percent.
  • the process of United States Patent 5,830,246 is utilized to dry such coal.
  • a drying process for preparing an irreversibly dried coal is used wherein a fluidized bed reactor is provided that has a fluidized density of about 10 to about 40 pounds per cubic foot. The fluidized bed reactor is maintained at a temperature of about 400-650 degrees Fahrenheit while coal with a moisture content of about 5 to about 30 percent and a combined oxygen content of from about 10 to about 20 percent is feed thereto.
  • mineral oil with an initial boiling point of at least about 900 degrees Fahrenheit is fed into the reactor about 0.5 to about 3.0 percent by weight of dried coal, thereby producing a coated coal.
  • the coated coal is then held at a temperature from about 400-650 degrees Fahrenheit in said reactor for about 1 to about 5 minutes while simultaneously comminuting and dewatering the coated coal.
  • the coated coal After the coated coal is exposed to an ambient environment at about 25 degrees Centigrade (about 77 degrees Fahrenheit) and a relative humidity of 50 percent, the coated coal contains less than about 2.0 percent of moisture by weight of coal, at least about 80 weight percent of the particles of said coated coal are smaller than 74 microns, and the coal has a combined oxygen content of from about 10 to about 20 weight percent.
  • the process the '247 patent is used in order to prepare the dried subbituminous coal. More specifically, one embodiment of the present invention employs a process for preparing an irreversibly dried coal with a first fluidized bed reactor with a fluidized bed density of about 20 to about 40 pounds per cubic foot, wherein the reactor is maintained at a temperature of about 150 to about 200 degrees Fahrenheit. Coal with a moisture content of about 15 to about 30 percent, an oxygen content of about 10 to about 20 percent, and a particle size such that all of the coal particles in such coal are in the range of from 0 to 2 inches are fed into the reactor.
  • the coal in the reactor is then subjected to a temperature of about 150 to about 200 degrees Fahrenheit for about 1 to about 5 minutes while simultaneously comminuting and dewatering the coal.
  • the comminuted and dewatered coal is then passed to a second fluidized bed reactor with a fluidized bed density of about 20 to about 40 pounds per cubic feet, wherein the reactor is at a temperature of about 480 to about 600 degrees Fahrenheit.
  • the second fluidized bed reactor is also fed mineral oil with an initial boiling point of at least about 900 degrees Fahrenheit of about 0.5 to about 3.0 weight percent by weight of dried coal, thereby producing a coated coal.
  • the coated coal is subjected to a temperature of about 480 to about 600 degrees Fahrenheit for about 1 to about 5 minutes while simultaneously comminuting and dewatering the coated coal, whereby a comminuted and dehydrated coal is produced.
  • the drying step 10 is critical in order to obtain a stable slurry. It should be noted that other coals often do not require such a drying step in order to produce a stable slurry.
  • United States patent 4,282,006, (the ⁇ 06 patent), the entire disclosure of which is hereby incorporated by reference herein, discloses the preparation of a 75 weight percent coal-water slurry using coal from the Black Mesa mine is described (see Example 3).
  • the Black Mesa coal does not have a combined oxygen content of from about 10 to about 25 percent. If the Black Mesa coal did have such an oxygen content, one of skill in the art would not have been able to make a stable slurry by drying. It has been discovered that, when coal with an oxygen content of about 10 to about 25 percent is mixed with a sufficient amount of water to produce a slurry with a solids content of about 65 to about 75 weight percent, such slurry is often not stable. When such coal is first dried and then modified in accordance with the process of Fig. 1 , a stable slurry may often be made from such coal.
  • step 12 after the dried coal has been produced in step 10, it is subject to a sieving operation in step 12 to remove oversize particles. For example, in such an operation all particles greater than about 700 microns are removed. In another embodiment, all particles greater than about 500 microns are removed.
  • the oversize particles are then fed via line to a mill 16, wherein they are ground and then recycled via line 18 to the dry subbituminous coal supply 10.
  • the undersize particles are fed via line 20 to a mixer 22 wherein a sufficient amount of water is added via line 24 to produce a coal/water mixture with a solids content by weight of dry coal of about 65 to about 75 weight percent.
  • a dispersing agent and/or an electrolyte may be added in accordance with the process described in the '006 patent.
  • the sieved, dried coal is then fed via line 26 to a mill 28, for example, a ball mill, in which the coal is ground to the particle size distribution described in the ⁇ 06 patent.
  • the coal is ground until at least about 5 weight percent of its particles are of colloidal size, and until a coal compact is produced that is described by the "CPFT" formula set forth in claim 1 the ⁇ 06 patent.
  • one or more other coal compacts may be added to the mill 28 via a line 30, and/or water and/or surfactant and/or electrolyte may be added.
  • the coal-water slurry produced in the mill 28 is also deashed 32.
  • the deashing process described in United States patent 4,468,232 is used, the entire disclosure of which is hereby incorporated by reference herein.
  • One embodiment of the present invention employs a process for preparing a clean coal-water slurry wherein a coal-water mixture comprised of about 60 to about 80 volume percent of solids that are grinded until a coal-water slurry is produced.
  • the contemplated slurry has a yield stress of about 3 to about 18 Pascals and a Brookfield viscosity at a solids content of 70 volume percent at ambient temperature and pressure, and a shear rate of 100 revolutions per minute of less than 5,000 centipoise.
  • the slurry is comprised of a consist of finely divided particles of coal dispersed in water wherein the specific surface area of about 0.8 to about 4.0 square meters per cubic centimeter and an interstitial porosity of less than about 20 volume percent.
  • about 5 to about 70 weight percent of said finely divided particles of coal in the water are of colloidal size, being smaller than about 3.0 microns.
  • finely divided particles of coal has a particle size distribution substantially in accordance with the following formula:
  • CPFT is the cumulative percent of said solid carbonaceous material finer than a certain specified particle size D, in volume percent;
  • (b) k is the number of component distributions in the compact and is at least 1 ;
  • Xj is the fractional amount of the component j in the compact, is less than or equal to 1.0, and the sum of all of the Xj's in the consist is 1.0;
  • N is the distribution modulus of fraction j and is greater than about 0.001 ;
  • D is the diameter of any particle in the compact and ranges from about 0.05 to about 1 180 microns;
  • Ds is the diameter of the smaller particle in fraction j, as measured at 1% CPFT on a plot of CPFT versus size D, is less than DL, and is greater than 0.05 microns;
  • (g) DL is the diameter of the size modulus in fraction j, measured by sieve size or its equivalent, and is from about 15 to about 1 180 microns.
  • At least about 85 weight percent of the coal particles in the consist have a particle size less than about 300 microns.
  • the net zeta potential of said colloidal sized particles of coal is about 15 to about 85 millivolts. The coal is cleaned after the cool water slurry is produced.
  • Fig. 2 is a flow diagram of a multi stage process 50 for drying coal of one embodiment.
  • the coal used in process 50 is similar to the coal described in column 1 (see lines 16-61 of column 3) of the '265 patent, with the exception that it preferably contains from about 15 to about 40 weight percent of moisture, may contain from about 10 to about 25 weight percent of combined oxygen, and may contain from about 10 to about 25 weight percent of ash.
  • coal used in process 50 may be lignitic or sub-bituminous coal.
  • coal used in step 52 is 2"x0", and more preferably, 2" by 1/4" or smaller.
  • 2" by 1/4" coal has all of its particles within the range of about 0.25 to about 2.0 inches.
  • Crushed coal conventionally has an about 2"x0" to 3" x 0" particle size distribution. This crushed coal can advantageously be used in at least some of the process disclosed herein.
  • raw coal is fed into a first reactor and is shown as step 52 wherein the raw coal is preferably fed from a feeder 102 (see Fig. 3; also see Fig. 4).
  • the feeder 102 may be similar to, or identical to the feeder 12 described in the '265 patent, i.e., any coal feeder commonly used in the art.
  • the feeder of one embodiment is comprised of a hopper and a star feeder. It is also contemplated that feeder be capable of continually delivering coal to fluidized bed.
  • the star feeder is a metering device that may be operated by a controller that controls the rate of coal removal from a hopper; see, e.g., U.S. Pat. No. 5,568,896, the entire disclosure of which is hereby incorporated by reference into this specification.
  • air is introduced into the first fluidized bed reactor 110 via line 106.
  • the air may be introduced by conventional means such as, e.g., a blower (not shown).
  • the air so introduced is hot air at a temperature of about 250 to about 400 degrees Fahrenheit, and preferably of about 300 to about 350 degrees Fahrenheit.
  • the air is introduced via line 106 into a fluidized bed 112 in order to maintain the temperature of such fluidized bed 112 at a temperature of about 300 to about 550 degrees Fahrenheit and, preferably of about 450 to about 500 degrees Fahrenheit.
  • this hot air helps oxidize a portion of the coal in the first reactor 1 10, thereby supplying energy required to vaporize the water in such coal. It is also believed that this oxidation occurs on the most reactive sites on the coal which reduces the natural equilibrium moisture thereof.
  • Equilibrium moisture is defined as the amount of water that will chemically combine with the coal and is measured by ASTM procedure D 1412. Reducing the equilibrium moisture of the coal reduces the amount of water the coal can absorb from the environment which reduces the tendency to self-heat that can result in spontaneous combustion of the coal.
  • the air is introduced via line 106 into fluidized bed 1 12 at a fluidizing velocity in the reactor vessel of greater than about 4 feet per second; the air is injected and preferably greater than about 5 feet per second. In one aspect of this embodiment, the air is introduced via line 106 at a fluidizing velocity of from about 5 to about 8 feet per second. In another aspect of this embodiment, the air is introduced via line 6 at a fluidizing velocity of from about 6 to about 8 feet per second. Without wishing to be bound to any particular theory, it is believed that maintaining the air flow within the desired ranges is essential for maintaining the desired conditions within the fluidized bed 112 and for conducting an efficient drying operation.
  • the reactor 110 is fluidized, i.e., a fluidized bed is established therein.
  • a fluidized bed is established by conventional method such as, e.g., the method disclosed in the '265 patent.
  • the fluidized bed 14 is provided in a reactor vessel 10 and is comprised of a bed of fluidized coal particles, and it preferably has a density of from about 20 to about 40 pounds per cubic foot. In one embodiment, the density of the fluidized bed 20 is from about 20 to about 30 pounds per cubic foot.
  • the fluidized bed density is the density of the bed while its materials are in the fluid state and does not refer to the particulate density of the materials in the bed.
  • the fluidized bed may be provided by any of the means well known to those skilled in the art. Reference may be had, e.g., to U.S. Patent Nos. 5,145,489, 5,547,549, 5,546,875 (heat treatment of coal in a fluidized bed reactor), U.S. Pat. No. 5,197,398 (separation of pyrite from coal in a fluidized bed), U.S. Pat. No. 5,087,269 (drying fine coal in a fluidized bed), U.S. Pat. No. 4,571,174 (drying particulate low rank coal in a fluidized bed), U.S. Pat. No.
  • the reactors 110 and 138 are often cylindrical and may be large when used with one-stage processes and often require gas velocities of about 18 feet per second or more. Without wishing to be bound to any particular theory, it is believed that velocities of this magnitude often result in excessive entrainment of the fluidized bed and/or may distort the fluidization in the fluidized bed. In any event, velocities of this magnitude do not produce the drying results obtained by embodiments of the present invention.
  • the fluidized bed 112 is heated by conventional means such as, e.g., using hot air provided in another reactor (not shown) and/or another device.
  • hot air provided in another reactor (not shown) and/or another device.
  • the fluidized bed is preferably maintained at a temperature of about 150 to about 200 degrees Fahrenheit.
  • the fluidized bed 14 is maintained at a temperature of about 165 to about 185 degrees Fahrenheit.
  • Various means may be used to maintain the temperature of fluidized bed 14 at a temperature of from about 150 to about 200 degrees Fahrenheit.
  • an internal or external heat exchanger not shown. See, e.g., U.S. Pat.
  • hot gas from, e.g., a separate fluidized bed reactor 18 is fed via line 20 into fluidized bed 14.
  • This hot gas preferably is at temperature of about 480 to about 600 degrees Fahrenheit and, more preferably, at a temperature of about 525 to about 575 degrees Fahrenheit.
  • the air fed via line 6 is hot air provided by a heat exchanger, not shown.
  • a heat exchanger not shown.
  • step 74 the heating of the fluidized bed 113 in reactor 138.
  • the air fed into reactor 113 is preferably fed at a velocity of from about 8 to about 12.2 feet per second. Without wishing to be bound to any particular theory, it is believed that this rate of air flow in reactor 138 is essential to maintain the fluidized bed under the desired conditions and to obtain the desired efficiency of drying; the use of lower or higher air flow velocities is undesirable and ineffective.
  • step 62 of the process coal "fines" are removed from the reaction mass disposed within the fluidized bed 112.
  • the finer coal portions i.e., those with a particle size less than about 400 microns
  • the coarser component of the entrained stream will preferably be cooled in cooler 128, as are the coarser components from cyclone 124.
  • the finer fraction from cyclone 120 is preferably passed via line 122 to cyclone 124.
  • the coarser component from cyclone 124 is then fed to cooler 128 and the fraction so cooled is then passed to storage 132.
  • the exhaust gas fed via line 134 is blended with the air in line 108 and the blended hot gases are then fed into the reactor 138.
  • One may use any of the cyclones conventionally used in fluid bed reactors useful for separating solids from gas.
  • one may use as cyclone, the cyclones described in U.S. Pat. No. 5,612,003 (fluidized bed with cyclone), U.S. Pat. No. 5,174,799 (cyclone separator for a fluidized bed reactor), U.S. Pat. Nos. 5,625,119, 5,562,884, and the like.
  • the entire disclosure of each of these United States patents is hereby incorporated by reference herein.
  • Water in reactor 110 is removed from the coal fed via line 104. This step is also indicated, as step 68, in Fig. 2.
  • the raw coal fed via line 104 of one embodiment contains from about 15 to about 40 weight percent of water.
  • the coal withdrawn via line 136 contains about 40 to about 60 percent less water. Put another way, the ratio of the water concentration in the raw coal divided by the water concentration in the dry coal is at from about 1.6 to about 2.5.
  • the water removed from the coal within the reactor 110 is passed together with flue gas and fines via line 118 to cyclone 120 and thence, via line 122 to cyclone 124. Thereafter, it passes via line 134 to condenser 135, wherein it is removed.
  • the gas passing from condenser is preferably substantially dry, containing less than about 5 weight percent of water. Thereafter, this dry gas is mixed with the air in line 108 and thence fed into the fluidized bed 113 as its fluidizing medium.
  • the raw coal from feeder 102 is maintained in reactor 110 for a time sufficient to remove from about 40 to about 60 weight percent of the water in the raw coal. Generally, such "residence time" is preferably less than about 15 minutes and frequently is from about 5 to about 12 minutes.
  • step 60 the dried coal from reactor 1 10 is removed from such reactor and fed into reactor 138 via line 136. Simultaneously, or sequentially, in step 72 exhaust gas is fed via line 108 from line 106, and is preferably mixed with dry gas from condenser 135, and it is then fed into fluidized bed 1 13.
  • the fluidized bed 1 13 is heated to a temperature that preferably is at least about 50 degrees Fahrenheit, higher than the temperature at which fluidized bed 1 12 is maintained.
  • the temperature in fluidized bed 1 13 preferably is about 450 to about 650 degrees Fahrenheit and, more preferably, about 550 to about 600 degrees Fahrenheit.
  • the fluidized bed 113 is preferably heated by both the hot coal fed via line 136, and/or the heat in the gas fed via line 108, and/or the combustion processes involved in said fluidized bed (often referred to as "off gas").
  • water is removed from the coal in fluidized bed 113, and such coal is then discharged via line 154; in general, the water content of such coal is preferably less than about 1 weight percent.
  • the water removed from the coal in reactor 138 is fed via line 140 (together with "fines” and as) to cyclone 142 and thence via line 144 to a condenser 146; the waste water from condenser 146 is then removed via line 150.
  • This step is depicted as step 84 in Fig. 2.
  • step 76 the fines are removed from the reactor 138 via line 140.
  • the solid product from cyclone 142 is then fed via line 152 and preferably blended with the dry coal from line 154.
  • the blend is then fed to cooler 156, wherein it is preferably cooled to a temperature less than 200 degrees Fahrenheit.
  • cooling is accomplished by immediately subjecting the product as it exits the fluid bed to a water spray of sufficient quantity to cool the blend and replace a portion of the blend's equilibrium moisture.
  • only a portion of the needed water is added at the exit of the reactor and the remaining amount is added in the cooler.
  • This cooler could be any number devices that facilitate adding water and mixing the product e.g. a mixing screw conveyor as manufactured by Austin Mac, Inc.
  • cooler that incorporates indirect cooling surfaces such as a hollow flight screw conveyor as manufactured by the Therma-Flite Company of 849 Jackson Street, Benica, California 94510 or a Roto-Tube cooler as manufactured by FMC Corporation of 400 Highpoint Drive Chalfont, PA 18914 is used to cool the product before water is added to replace a portion of the equilibrium moisture. After cooling the blend is fed via line 158 to storage.
  • indirect cooling surfaces such as a hollow flight screw conveyor as manufactured by the Therma-Flite Company of 849 Jackson Street, Benica, California 94510 or a Roto-Tube cooler as manufactured by FMC Corporation of 400 Highpoint Drive Chalfont, PA 18914 is used to cool the product before water is added to replace a portion of the equilibrium moisture. After cooling the blend is fed via line 158 to storage.
  • Fig. 4 is a schematic of a preferred apparatus which is similar to the apparatus depicted in Fig. 2 but utilizes a single, compartmentalized vessel instead of the two reactor vessels 110 and 138.
  • Fig. 5 is an alternate embodiment of the present invention wherein the coal product is cooled after it exits the second fluidized bed 38.
  • the temperature of the coal product is sensed by a temperature sensor 160 as the coal is directed to a water spray 102 that cools the coal product to a temperature less than the ambient boiling point of water (212 degrees Fahrenheit at sea level).
  • the water spray may be continuous and/or be selectively controlled by a rotary valve 164 motor that is indexed to open a solenoid valve to inject water.
  • the temperature of the coal product is also sensed by sensor 160 after being cooled.
  • the coal may be further cooled in a screw 168, which will be described in further detail below with reference to Figs. 6-8.
  • the contemplated temperature sensors can be any temperature sensing device, but, preferably an optical sensor.
  • One of skill in the art will appreciate that although one embodiment employs water to cool the coal other cooling techniques may be employed, such as direct contact cooling that may use an inert gas or a heat exchanger, without departing from the scope of the invention.
  • Fig. 6 is a schematic of a preferred coal drying system 210 wherein feed coal is received at the site of the system 210 by railcar, by truck, or in Super Sacks.
  • the feed coal may contain, e.g., up to about 40 weight percent of moisture.
  • the coal used in the process and system has an equilibrium moisture of about 18 to about 26 percent.
  • equilibrium moisture is the amount of moisture in the coal that is bonded to the atoms in the coal and is measured by ASTM procedure D1412.
  • the coal is fed into feed hopper 214.
  • the feed hopper 214 is a custom feed hopper equipped with a 6 inch Plattco rotary valve 212 (manufactured by the Plattco Corporation of 7 White Street, Plattsburgh, New York 12901 ) at its bottom that is adapted to controllably feed coal to the feed conveyor 218.
  • valve 212 is connected via a link (not shown) to a controller (not shown).
  • the coal is fed directly into a coal surge bin 220 from a railcar or truck unloading station (not shown) by a conveyor belt (not shown).
  • the rotary valve 212 empties coal onto a conveyor 218 that, in part runs underneath the feed hopper 214.
  • the feed conveyor 218 is New London Feed Conveyor clearing about 34 feet and capable of providing about 6000 pounds per hour of coal; this feed conveyor is manufactured by the New London Engineering Company of 1700 Division Street, New London, Wisconsin. 54961.
  • the feed conveyor 218 carries the coal to a coal surge bin 220 equipped with a coal feed screw 222 at its bottom that is preferably speed controlled and adapted to supply the desired amount of coal at the desired rate to the reactor.
  • a coal feed screw 222 instead of coal feed screw 222 one could use a rotary valve or lock hoppers if the surge bin was above the reactor.
  • the coal to fill the surge bin may come directly from a coal receiving facility (not shown).
  • the coal surge bin 220 is comprised of low level and high level sensors (not shown) that automatically control the rotary valve 212 located underneath the feed hopper 214 in order to maintain a minimum amount of feed coal in the surge hopper.
  • the coal surge bin 220 level is controlled using a continuous level sensor such as, e.g., an ultrasonic level sensing unit.
  • the feed screw 222 feeds coal via line 224 to fluid bed reactor 226.
  • the fluid bed reactor may be a custom design or a commercially available design e.g. fluid bed reactor model C-FBD-36/72 by Carrier Vibrating Equipment, Inc. PO Box 37070, Louisville, Kentucky.
  • the coal prior to the time the coal is fed to reactor 226 it is dried to a moisture content of less than about 40 weight percent and, more preferably, less than about 30 weight percent.
  • the coal may be pre-dried by conventional means including, e.g., rotary kilns (see, e.g., United States patent 5,103,743 of Berg), cascaded whirling bed dryers (see, e.g., United States patent 4,470,878 of Petrovic et al.), elongated slot dryers (see, e.g., United States patent 4,617,744 of Siddoway et al.), hopper dryers (see, e.g., United States patent 5,033,208 of Ohno et al.), traveling bed dryers (see.
  • rotary kilns see, e.g., United States patent 5,103,743 of Berg
  • cascaded whirling bed dryers see, e.g., United States patent 4,470,8
  • the heat source for pre-drying the coal may be of the form of waste heat, other available heat sources, or auxiliary fuels.
  • the coal is pre-dried to a moisture content of about 12 to about 20 weight percent.
  • two or more coals, each with different moisture contents, are blended together to provide a raw coal feed with a moisture content of less than about 40 weight percent.
  • the raw coal is spread with a coal spreader and contacted with, e.g., off-gas from the fluidized bed reactor in order to dry it to the desired moisture content.
  • Figure 7 is a schematic of an integrated fluid bed and coal pre-dryer system 300 comprised of a fluidized bed 302 and a spreader 304.
  • a feed screw 308 feeds the raw coal via line 310 onto the spreader 304.
  • the spreader 304 distributes the incoming coal so that off gases from the fluidized bed 302 that flow, e.g., in the directions of arrows 306 contact and pre-dry the coal prior to the time it reaches the fluidized bed 302.
  • the reactor 226 is fluidized, i.e., a fluidized bed is established therein.
  • a fluidized bed is established therein.
  • the fluidized bed reactor is cylindrical and has an aspect ratio (bed height divided by diameter) of 2 or less; in one embodiment, the aspect ratio ranges from about 6/3 to about 1/3.
  • the bed within the cylindrical fluidized bed reactor preferably has a depth of from about 1 to about 8 feet and, more preferably, from about 2 to about 4 feet.
  • Non-cylindrical fluidized beds also may be used, but in one embodiment, the aspect ratio thereof (the ratio of the bed height to the maximum cross sectional dimension) ranges from about 2/1 to about 1/3.
  • Non-cylindrical fluidized beds may also include enlarged upper sections to facilitate particle disengagement, e.g., fluid bed reactor model C-FBD-36/72 by Carrier Vibrating Equipment, Inc. PO Box 37070, Louisville, Kentucky.
  • Bed fluidization may be achieved by fluidizing gas that enters the reactor 226 through a perforated plate (not shown). Fresh air is used for fluidizing, but a mixture of fresh air and recycle gas may be used. It is preferred to use one blower to control the amount and the composition of the fluidizing gas. In other embodiments, multiple blowers may be used.
  • One embodiment employs a startup heater air fan system 228 that provides the air for an in-duct, natural gas-fired burner used for preheating the fluidizing gas during startup.
  • the startup heater air fan system 228 may, e.g., be a blower provided with a burner system that is manufactured by, e.g., Stelter & Brinck, Ltd., 201 Sales Avenue, Harrison, Ohio 45030.
  • a recycle fan 230 is used to move the fluidized gas in a loop comprised of lines 232, 234, 236, 238, 240, 242, 244, 252, and 254.
  • the recycle fan 230 may be, e.g., a New York Blower Type HP Pressure Blower manufactured by The New York Blower Company.
  • a fresh air fan 256 is used to add fresh air to the fluidizing gas in order to adjust the oxygen content of the fluidizing gas.
  • the fresh air fan 256 may, e.g., be a New York Blower Type 2606 Pressure Blower manufactured by The New York Blower Company.
  • the fan 256 may be replaced with a control valve and a suitable control valve added to line 252.
  • a vent valve 264 is used to release an equal amount of gas to the emissions control device 270 to maintain a consistent flow of fluidizing gas through the reactor.
  • the velocity of the fluidizing gas is less than about 12 feet per second and, preferably, from about 4 to about 9 feet per second.
  • Gases exiting the reactor 226 enter a dust removal device 262 where coal fines are separated;
  • the dust removal device may be, e.g., a Flex-Kleen Pulse Jet Baghouse manufactured by the Flex Kleen Division of the Met Pro Corporation of Glendale Heights, Illinois or a cyclone e.g., manufactured by Fisher-Kloterman, Inc., (a CECO Environmental Company) of 822 South 15th Street, Louisville, Kentucky 40210.
  • Clean gas passes a vent valve 264 where an appropriate amount of gas is vented to an emissions control device 270 and the balance becomes a part of the "closed loop recirculation.”
  • the purpose of the emissions control device is to destroy any carbonaceous components in the offgas after removal of particulate.
  • the emissions control device could be, e.g., a thermal oxidizer manufactured by John Zink Company, LLC of 1 1920 East Apache, Tulsa, Oklahoma 74116.
  • the emissions control device could be, e.g., a catalytic oxidizer manufactured by Catalytic Product, International of 980 Ensell Road, Lake Zurich, Illinois 60047-1557.
  • the emissions control device could also be a gas turbine where extra fuel is added to the gas to raise the temperature and the gases are then expanded to generate electricity for the plant use or for sale to the utility.
  • a typical startup procedure involves, e.g., starting the heater air fan 228 and the recycle fan 230.
  • Recycle fan speed is selected to ensure sufficient gas flow to achieve bed fluidization.
  • Coal feed is started to fill the reactor 226 to the desired bed height.
  • An indication of a full bed is overflow of coal from the reactor 226 to the screw cooler.
  • An in-duct natural gas-fired burner 266 is started, and the temperature of the fluidizing gas is slowly increased.
  • the burner 266 may be, e.g., a Stelter & Brink 2,000,000 btu per hour process air heater.
  • the reactor 226 is preferably equipped with several water spray nozzles (not shown) to assist in the control the temperature of the fluidized bed.
  • the reactor is also preferably equipped with several temperature sensors to monitor the temperature of the fluidized bed. In case of emergency, dump valve 66 can be actuated to quickly empty the reactor contents into the cooler 260.
  • the gases leaving the reactor 226 via line 244 have an oxygen content of less than 15 volume percent, whereas the oxygen content of the fluidizing gas is maintained at greater than about 15 volume percent (and, more preferably, closer to that of fresh air) to maximize the rate of coal processing.
  • the temperature of the fluidized bed is maintained at about 450 to about 650 degrees Fahrenheit and, more preferably, at about 580 to about 620 degrees Fahrenheit.
  • the amount of heat released via the combustion of the coal is balanced by the amount of heat required to heat and dry the coal added to the reactor.
  • the temperature of the fluidized bed can be controlled by varying the rate of coal feed into the system, by the amount of oxygen supplied to the system through the fluidizing gas and/or by injection of water in the fluidized bed.
  • the off gas from reactor 226 is run through a particle separation step to remove particles entrained in the reactor offgas.
  • this step consists of a single baghouse such as baghouse 262 or a cyclone (not shown).
  • the particle separation step includes multiple devices to facilitate recovery of entrained particles on the basis of particle size or density. Larger particles may be directed to the cooler for recovery as coal product.
  • the coal produced in reactor 226 is typically at a temperature of about 580 to about 620 degrees Fahrenheit, and it typically contains about 0 to about 2 weight percent of moisture.
  • This product is discharged through feeder 268 which may be, e.g., a rotary valve, lock hoppers, to a cooling/rehydration step.
  • feeder 268 may be, e.g., a rotary valve, lock hoppers, to a cooling/rehydration step.
  • This hot, substantially dry coal is then cooled and partially rehydrated in the next step of the process.
  • the cooling, rehydration and stabilizing step can be applied to coal produced via the process described herein above. Alternatively, or additionally, it can be applied to heated, and partially or fully dried coal produced by other processes. Thus, e.g., one may produce such a heated, partially dried coal using one or more of the processes described in the above-identified patents related to the drying of coal.
  • the preferred method for cooling, rehydration, and stabilization occurs in one process piece of process equipment 260.
  • This could be a screw conveyor, a rotary drum, rotary tube cooler or any other device that would provide cooling through heat transfer surfaces and or the application of water as well as mixing.
  • This cooler 260 would be equipped with a multiplicity of water sprays and temperature sensors to allow water to be applied to the product for either progressively lowering the temperature of the product to less than the ambient boiling point of water (212 degrees Fahrenheit at sea level) and/or adding about 5 to 12 percent moisture to the product.
  • the application of water may be continuous or intermittent.
  • the control of water application could be on the basis of temperature, the mass flow rate of product and/or a combination thereof.
  • One of skill in the art will appreciate that the apparatus shown in Fig. 5 may generally be employed.
  • the cooling, rehydration and stabilization device would be a hollow flight screw cooler as manufactured by the Therma-Flite Company of 849 Jackson Street, Benica, California 94510.
  • Fig. 8 is a schematic of a hollow-flight screw cooler 400 that is comprised of a chamber 402, a hollow screw 404 disposed in the center of said chamber, a device for rotating the hollow screw (not shown), a hollow jacket 406 disposed around said chamber, a first cool water inlet port 408, a second cool water inlet 410, a first hot water outlet 412, and a second hot water outlet 414.
  • the rotating screw assembly 404 is comprised of a hollow shaft 418 and a multiplicity of hollow flights 420. Cold water is fed into inlet port 408 and exchanges heat with the material that contacts the flights 420 and the shaft 418. Cold water is also fed into jacket inlet port 410 and exchanges heat with the material that contacts the chamber 402.
  • the hollow-flight screw cooler assembly 400 is comprised of a multiplicity of temperature sensors 420 that are adapted to sense the temperature at various points in the screw assembly.
  • the screw cooler assembly is also comprised of a multiplicity of water sprays 424.
  • the goal is to reduce the temperature of the hot coal received in from the reactor from a temperature of about 580 to about 620 degrees Fahrenheit to a temperature of less than about 250 degrees Fahrenheit using heat exchange surfaces 420, 418 and 402 described above.
  • Using a heat exchange device for the initial cooling slows the rate of heat removal from the product which reduces thermal shock and may improve the mechanical integrity of the product coal.
  • Further cooling of the product to a temperature between about 170 degrees Fahrenheit and about 200 degrees Fahrenheit is obtained using direct application of water using the water sprays 424.
  • the direct application of water also enhances the stability of the product by restoring the moisture content of the coal to equilibrium moisture content, a value typically in the about 6 to 12 weight percent range.
  • the multiplicity of temperature sensors and/or the mass flow rate of the product are used to control the water sprays 424.
  • the temperature sensors may also be used as a part of the overall process control. For example, if the rate of temperature decrease in the hollow-flight screw cooler is too low, and/or too high, the rate may be modified by modifying the coal feed rate into the system, and/or by modifying the rate at which the screw turns and/or the rate at which cooling water is circulated and/or the rate at which water is applied using the sprays.
  • the water is preferably sprayed onto the coal after it has reached a temperature of less than about 250 degrees Fahrenheit.
  • the water spray may be continuous, and/or it may be intermittent. In one preferred embodiment, water is introduced only in the last half of the hollow-flight screw cooler assembly 400.
  • the water sprayed into the system has at least two functions. The first is to cool the coal by transferring heat from the coal to the water and possibly vaporizing some of the water. The second function of the sprayed water is to rehydrate the coal until it preferably contains about 6 to about 12 weight percent of moisture.
  • the rehydration step in that regard pacifies the processed coal against further hydration.
  • the water so introduced preferably reduces the temperature of the coal to less than 212 degrees Fahrenheit.
  • water is introduced only in the last half of the hollow-flight screw cooler assembly such that the coal at the outlet port 422 is at less than 180 degrees Fahrenheit.
  • the cooled rehydrated and stabilized coal from cooler 260 is discharged via line 270 to conveyor 272.
  • the conveyor 272 conveys the dried rehydrated stable coal to a storage system 274 (not shown), a load out system for trucks or railcars, or directly to the end user. Any gases emitted in the hollow-flight screw cooler are directed to the emissions control device 270.
  • the coal produced in the process of the invention shown in Figs. 6- 8 contains about 36 to about 39 weight percent of volatile matter and about 50 to about 65 weight percent of fixed carbon, and such coal has a heating value of about 9,300 to about 1 1 ,000 btu (British thermal units) per pound.
  • the coal produced in the process of the invention preferably contains about 6 to about 12 weight percent of moisture. It is "irreversibly dried," i.e., its equilibrium moisture is reduced from the native coal which reduces its tendency to absorb moisture. The coal is stabilized wherein 50 to 100 percent of the equilibrium moisture is added back to the dry coal product to minimize the reaction rate and heat generation associated with moisture absorption.
  • a vibrating fluidizing bed is utilized in assembly 10.
  • This type of fluidizing bed is well known to those skilled in the art and is described, e.g., in United States patent 4,444,129 (the ⁇ 29 patent), the entire disclosure of which is hereby incorporated by reference into this specification.
  • the ' 129 patent discloses a process for drying wet coal fines smaller than 28 mesh in size that employs both a vibrating fluidized bed type dryer and a coal fired burner for supplying hot drying gases to the dryer.
  • a regenerative separator is interposed between the coal fired burner and the fluidized bed type dryer to satisfactorily remove particle matter from the gases without unacceptable pressure losses. Hot gases exhausted from the fluidized bed type dryer are also cleansed to remove particulate coal particles which are used as fuel for the coal fired burner.
  • a method of drying fine coal particles smaller than approximately 28 mesh in size wherein gases are heated by a coal fueled burner.
  • the heated gases are passed through a regenerative separator to remove substantially all particulate ash particles therefrom to prevent ignition of the coal particles.
  • the passing coal particles are passed from an inlet to an outlet of a fluidized bed type dryer wherein the gases from the regenerative separator are directed through the fluidized bed dryer to dry the coal particles as they are passed therethrough.
  • the dried coal particles are collected for future use as fuel and the bulk of the gases are recirculated to the burner prior to passing the gases through the regenerative separator, gases not recirculated being limited to that amount required to discharge water equivalent to that removed from the coal stream to be dried.
  • passing the heated gases through the regenerative separator includes providing rotational movement to the gases by intersecting curved blades positioned in the path of the heated gases, and removing the ash particles during the rotation of the gases through the side of the separator. Further, at least a portion of the gases to collect particulate coal exhausted from the dryer and utilizing the collected particulate coal to fuel the coal fueled burner. In addition, at least some of the coal particles from gas exhausted from the dryer for mixing with dry coal paths delivered through the outlet of the dryer. The rotational movement of the gases may also be stopped in the regenerative separator before entry into the fluidized bed dryer, by intersecting blades curved in the opposite direction from the rotation.
  • fluidizing gas may be introduced into the fluidized bed reactor 226 (and, in particular, into the fluidized bed thereof) at a fluidizing velocity in the reactor vessel of greater than about 4 feet per second and, more preferably, greater than about 5 feet per second.
  • the fluidizing gas is introduced at a fluidizing velocity of about 5 to about 8 feet per second.
  • the fluidizing gas is introduced at a fluidizing velocity of about 6 to about 8 feet per second.
  • the fluidized bed reactor 226 is a cylindrical reactor that may be heated by conventional means such as, e.g., using hot air provided in another reactor (not shown) and/or another device.
  • the fluidized bed 214 is preferably maintained at a temperature of about 150 to about 200 degrees Fahrenheit. In a more preferred embodiment, the fluidized bed 214 is maintained at a temperature of about 165 to about 185 degrees Fahrenheit.
  • Various means may be used to maintain the temperature of fluidized bed at its desired temperature. Thus, e.g., one may use an internal or external heat exchanger (not shown). See, e.g., U.S. Patent Nos. 5,537,941 , 5,471 ,955, 5,442,919, 5,477,850, 5,462,932, and the like which are incorporated by reference herein.
  • hot fluidizing gas from a heat exchanger may be fed to fluidized bed reactor 226.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Geology (AREA)
  • Geochemistry & Mineralogy (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • Microbiology (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Drying Of Solid Materials (AREA)

Abstract

L'invention porte sur un procédé de séchage du charbon, suivant lequel du charbon est amené à passer dans un réacteur à lit fluidisé et est chauffé à une température prédéterminée. Le charbon séché est ensuite adressé à un dispositif de refroidissement où la température du produit est réduite à approximativement 200 degrés Fahrenheit et de l'eau est ajoutée pour passiver encore le charbon.
PCT/US2010/049957 2009-09-24 2010-09-23 Procédé de séchage du charbon WO2011038089A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AU2010298284A AU2010298284B2 (en) 2009-09-24 2010-09-23 Process for drying coal
CA2780314A CA2780314A1 (fr) 2009-09-24 2010-09-23 Procede de sechage du charbon
EP10819441.6A EP2480641A4 (fr) 2009-09-24 2010-09-23 Procédé de séchage du charbon

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US12/566,174 2009-09-24
US12/566,174 US8197561B2 (en) 2001-10-10 2009-09-24 Process for drying coal

Publications (1)

Publication Number Publication Date
WO2011038089A1 true WO2011038089A1 (fr) 2011-03-31

Family

ID=43796200

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2010/049957 WO2011038089A1 (fr) 2009-09-24 2010-09-23 Procédé de séchage du charbon

Country Status (5)

Country Link
US (1) US8197561B2 (fr)
EP (1) EP2480641A4 (fr)
AU (1) AU2010298284B2 (fr)
CA (1) CA2780314A1 (fr)
WO (1) WO2011038089A1 (fr)

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2322473B1 (fr) * 2009-10-15 2012-07-25 Süd-Chemie AG Procédé de suppression d'un matériau à contamination particulaire dans un matériau à phosphate métallique au lithium mélangé à particules
JP4719298B1 (ja) * 2010-03-24 2011-07-06 三菱重工業株式会社 改質石炭製造装置
US9057037B2 (en) 2010-04-20 2015-06-16 River Basin Energy, Inc. Post torrefaction biomass pelletization
US8956426B2 (en) 2010-04-20 2015-02-17 River Basin Energy, Inc. Method of drying biomass
US20110314728A1 (en) * 2010-06-24 2011-12-29 River Basin Energy, Inc. Method of Simultaneously Drying Coal and Torrefying Biomass
JP4939662B1 (ja) * 2011-03-22 2012-05-30 三菱重工業株式会社 石炭改質システム
WO2014049587A1 (fr) * 2012-09-25 2014-04-03 Pt Total Sinergy International Dispositif pour la valorisation de matières organiques solides
AU2013350303B2 (en) * 2012-11-20 2018-07-05 Flsmidth A/S A dryer for drying a mineral sample
WO2014078886A1 (fr) * 2012-11-20 2014-05-30 Imp Group (Pty) Ltd Séchoir pour le séchage d'un échantillon de minerai
US9370758B2 (en) 2013-03-26 2016-06-21 Uop Llc Process for transferring catalyst and an apparatus relating thereto
US20150047253A1 (en) * 2013-08-16 2015-02-19 Kunimichi Sato Method for increasing calorific value of low-grade coals
US9738845B2 (en) * 2015-09-17 2017-08-22 Omnis Thermal Technologies, Llc Combustible pellet drying system
CN108647819A (zh) * 2018-05-09 2018-10-12 威特龙消防安全集团股份公司 一种煤堆管理系统
US10976049B2 (en) * 2019-03-22 2021-04-13 General Electric Company Hybrid boiler-dryer and method
DE202020100549U1 (de) * 2020-01-31 2020-02-20 Rematec Gmbh & Co. Kg Kühlvorrichtung

Citations (64)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3424573A (en) 1964-11-02 1969-01-28 Rocco Catoggio De Villiers Process for combined oxygen iron refining and producing of ferrous melts
US3687431A (en) 1970-12-18 1972-08-29 Aluminum Co Of America Preheating of dry aggregate for carbon electrodes
US4071151A (en) 1976-11-24 1978-01-31 The United States Of America As Represented By The United States Department Of Energy Vibratory high pressure coal feeder having a helical ramp
US4140228A (en) 1977-12-01 1979-02-20 The United States Of America As Represented By The United States Department Of Energy Dry piston coal feeder
US4142868A (en) 1978-05-02 1979-03-06 The United States Of America As Represented By The United States Department Of Energy Wear compensating seal means for rotary piston coal feeder
US4149228A (en) 1977-07-22 1979-04-10 The United States Of America As Represented By The Secretary Of The Army Compact uniform light diffuser and attenuator
US4282006A (en) 1978-11-02 1981-08-04 Alfred University Research Foundation Inc. Coal-water slurry and method for its preparation
US4300291A (en) 1979-03-13 1981-11-17 Salem Corporation Methods and apparatus for heating particulate material
US4324544A (en) 1980-06-12 1982-04-13 Fmc Corporation Process and system for drying coal in a fluidized bed by partial combustion
US4341530A (en) 1979-12-05 1982-07-27 The United States Of America As Represented By The Department Of Energy Slurry atomizer for a coal-feeder and dryer used to provide coal at gasifier pressure
US4353427A (en) 1980-09-26 1982-10-12 Stock Equipment Company Weight-sensor calibration for gravimetric coal feeder
US4430963A (en) 1982-12-03 1984-02-14 General Signal System for generating dry coal weight signal for coal feeder and control system based thereon
US4444129A (en) 1982-11-05 1984-04-24 Lecorp Method of drying fine coal particles
US4468232A (en) 1982-05-05 1984-08-28 Alfred University Research Foundation, Inc. Process for preparing a clean coal-water slurry
US4470878A (en) 1981-05-13 1984-09-11 Krupp-Koppers Gmbh Method for drying coal and cooling coke
US4486894A (en) 1979-08-07 1984-12-04 Coal Industry (Patents) Limited Method of and apparatus for sensing the ash content of coal
US4495710A (en) 1983-08-01 1985-01-29 Atlantic Richfield Company Method for stabilizing particulate low rank coal in a fluidized bed
US4497122A (en) 1982-02-25 1985-02-05 Fuller Company Rotary coal feeder and dryer
US4571174A (en) 1984-03-29 1986-02-18 Atlantic Richfield Company Method for drying particulate law rank coal in a fluidized bed
US4575418A (en) 1984-10-03 1986-03-11 The Dow Chemical Company Coal cleaning and the removal of ash from coal
US4606793A (en) 1981-06-11 1986-08-19 Vladan Petrovic Method for the operation of a carbonization plant
US4617744A (en) 1985-12-24 1986-10-21 Shell Oil Company Elongated slot dryer for wet particulate material
US4795037A (en) 1986-05-07 1989-01-03 Rich Jr John W Process for separating high ash coal from refuse
US4852384A (en) 1986-04-21 1989-08-01 The Babcock & Wilcox Company Automatic calibration and control system for a combined oxygen and combustibles analyzer
US5030054A (en) 1989-06-23 1991-07-09 Detroit Stoker Company Combination mechanical/pneumatic coal feeder
US5033208A (en) 1989-12-13 1991-07-23 Kabushiki Kaisha Matsui Seisakusho Hopper dryer
US5050310A (en) 1989-10-13 1991-09-24 Jiles Stephen L Plastic-pipe ovality gauge
US5087269A (en) 1989-04-03 1992-02-11 Western Research Institute Inclined fluidized bed system for drying fine coal
US5103743A (en) 1987-09-21 1992-04-14 A. Ahlstrom Corporation Method and apparatus for drying solid material
US5145489A (en) 1990-11-28 1992-09-08 Fuels Management Inc. Method for coprocessing coal and oil
US5171474A (en) 1990-01-22 1992-12-15 Kasei Optonix, Ltd. Method for treating a phosphor
US5174799A (en) 1990-04-06 1992-12-29 Foster Wheeler Energy Corporation Horizontal cyclone separator for a fluidized bed reactor
US5197398A (en) 1991-04-16 1993-03-30 Electric Power Research Institute Separation of pyrite from coal in a fluidized bed
US5265774A (en) 1992-12-29 1993-11-30 Combustion Engineering, Inc. Coal feeder with quick release cleanout door
US5322530A (en) * 1992-10-20 1994-06-21 Western Research Institute Process for clean-burning fuel from low-rank coal
US5327717A (en) 1991-02-05 1994-07-12 Deutsch-Voest-Alpine Industrieanlagenbau Gmbh Process for drying coal for melt-down or coal gasifiers
US5361513A (en) 1992-11-25 1994-11-08 Amax Coal Industries, Inc. Method and apparatus for drying and briquetting coal
US5396260A (en) 1992-12-22 1995-03-07 The Center For Innovative Technology Video instrumentation for the analysis of mineral content in ores and coal
US5411560A (en) 1992-11-05 1995-05-02 Swinburne Limited Method of producing binderless pellets from low rank coal
US5444733A (en) 1993-05-17 1995-08-22 Danieli & C. Officine Meccaniche Spa Electric arc furnace with alternative sources of energy and operating method for such electric furnace
US5442919A (en) 1993-12-27 1995-08-22 Combustion Engineering, Inc. Reheater protection in a circulating fluidized bed steam generator
US5462932A (en) 1994-05-17 1995-10-31 Merck & Co., Inc. Oral liquid alendronate formulations
US5471955A (en) 1994-05-02 1995-12-05 Foster Wheeler Energy Corporation Fluidized bed combustion system having a heat exchanger in the upper furnace
US5477850A (en) 1992-10-06 1995-12-26 Rockwell International Corp. Integrated buoyancy suit crew protection system with +/-GZ protection
US5503646A (en) 1994-06-30 1996-04-02 Fording Coal Limited Process for coal - heavy oil upgrading
US5521132A (en) 1994-09-01 1996-05-28 The United States Of America As Represented By The Secretary Of The Navy Ash-based ceramic materials
US5527365A (en) 1993-11-26 1996-06-18 National Research Council Of Canada Irreversible drying of carbonaceous fuels
US5534137A (en) 1993-05-28 1996-07-09 Reilly Industries, Inc. Process for de-ashing coal tar
US5537941A (en) 1994-04-28 1996-07-23 Foster Wheeler Energy Corporation Pressurized fluidized bed combustion system and method with integral recycle heat exchanger
US5546875A (en) 1993-08-27 1996-08-20 Energy And Environmental Research Center Foundation Controlled spontaneous reactor system
US5547549A (en) 1993-04-22 1996-08-20 Fraas; Arthur P. Vibrating bed coal pyrolysis system
US5562884A (en) 1990-04-17 1996-10-08 A. Ahlstrom Corporation Reducing N2 O emissions when burning nitrogen-containing fuels in fluidized bed reactors
US5568896A (en) 1994-02-22 1996-10-29 Beloit Technologies, Inc. Methods for preparing pulpwood for digestion
US5612003A (en) 1995-10-18 1997-03-18 Fisher-Klosterman, Inc. Fluidized bed wtih cyclone
US5625119A (en) 1992-06-22 1997-04-29 Successful Venture Enterprises Inc. Method for treating sludge and soil contaminated with hydrocarbons
US5637336A (en) 1994-04-29 1997-06-10 Kannenberg; James R. Process for drying malt
US5730775A (en) * 1994-12-16 1998-03-24 Midrex International B.V. Rotterdam, Zurich Branch Method for rapid reduction of iron oxide in a rotary hearth furnace
US5830247A (en) 1997-03-03 1998-11-03 Fuels Management, Inc. Process for processing coal
US5830246A (en) 1997-03-03 1998-11-03 Fuels Management, Inc. Process for processing coal
US5832848A (en) 1994-10-03 1998-11-10 Quality Heat Treatment Pty, Ltd. Fluidized bed heat treatment furnace
US5858035A (en) 1997-03-03 1999-01-12 Fuels Management, Inc. Process for processing coal
US5904741A (en) 1997-03-03 1999-05-18 Fuels Management, Inc. Process for processing coal
US20050188608A1 (en) 2001-10-10 2005-09-01 Dunlop Donald D. Process for drying coal
US20060096167A1 (en) * 2001-10-10 2006-05-11 Dunlop Donald D Process for in-situ passivation of partially-dried coal

Family Cites Families (75)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US459650A (en) * 1891-09-15 Tubular rivet and method of making the same
US1632829A (en) * 1924-08-14 1927-06-21 Fleissner Hans Method of drying coal and the like
DE569941C (de) 1930-05-23 1933-02-09 Emil Kahane Verfahren zur Veredlung von wasserreichen, insbesondere lignitischen Braunkohlen und aehnlichen minderwertigen Brennstoffen
US1960917A (en) * 1932-09-09 1934-05-29 Delaware Chemical Engineering Process of treating coal
US2197792A (en) * 1937-12-06 1940-04-23 John A Erickson Coal spraying chute
US2204781A (en) * 1939-07-27 1940-06-18 George M Wattles Art of protecting coal and like
US2610115A (en) * 1948-09-30 1952-09-09 Henry G Lykken Method for dehydrating lignite
US2811427A (en) 1952-09-08 1957-10-29 Henry G Lykken Lignite fuel
US3047473A (en) * 1956-09-10 1962-07-31 Allied Chem Drying, preheating, transferring and carbonizing coal
US4145256A (en) * 1970-10-21 1979-03-20 Georgia Tech Research Institute Method and apparatus for producing a carbonaceous residue product
US3723079A (en) * 1971-07-23 1973-03-27 Sun Research Development Stabilization of coal
CA959783A (en) 1972-01-28 1974-12-24 James G. Speight Method of preparation of coal for safe transport and storage
US3977947A (en) * 1972-07-26 1976-08-31 The Kingsford Company Fluidized bed carbonization
US3896557A (en) * 1974-05-09 1975-07-29 Sun Oil Co Delaware Process for drying and stabilizing coal
ZA743325B (en) * 1974-05-24 1976-02-25 South African Coal Oil Gas Improvements relating to a carbonaceous material
US3961914A (en) * 1974-07-26 1976-06-08 Hazen Research, Inc. Process for treating coal to make it resistant to spontaneous combustion
US3971639A (en) * 1974-12-23 1976-07-27 Gulf Oil Corporation Fluid bed coal gasification
US4052169A (en) 1975-02-20 1977-10-04 Texaco Inc. Treatment of solid fuels
US3997422A (en) 1975-06-20 1976-12-14 Gulf Oil Corporation Combination coal deashing and coking process
US3985517A (en) 1975-08-20 1976-10-12 Hydrocarbon Research, Inc. Coal passivation process
US3985516A (en) 1975-08-20 1976-10-12 Hydrocarbon Research, Inc. Coal drying and passivation process
US4104035A (en) * 1975-12-11 1978-08-01 Texaco Inc. Preparation of solid fuel-water slurries
US4043763A (en) * 1976-04-12 1977-08-23 Suntech, Inc. Stabilization of dried coal
US4192650A (en) * 1978-07-17 1980-03-11 Sunoco Energy Development Co. Process for drying and stabilizing coal
US4214875A (en) * 1978-07-31 1980-07-29 Atlantic Research Corporation Coated coal piles
US4213752A (en) * 1978-11-06 1980-07-22 Suntech, Inc. Coal drying process
US4170456A (en) 1978-11-22 1979-10-09 Atlantic Richfield Company Inhibiting spontaneous combustion of coal char
US4203727A (en) * 1978-11-29 1980-05-20 Simpson Charles H Process for reducing the sulfur content of coal
US4226371A (en) 1979-04-06 1980-10-07 Willams Robert M Inert grinding and direct firing in coal burning systems
JPS55145791A (en) * 1979-05-01 1980-11-13 Kobe Steel Ltd Reforming of coal
US4249909A (en) * 1979-05-30 1981-02-10 Hydrocarbon Research, Inc. Drying and passivating wet coals and lignite
DE7920101U1 (de) 1979-07-13 1979-10-31 Deutsche Babcock Ag, 4200 Oberhausen Entascher
AU530284B2 (en) * 1979-07-20 1983-07-07 Mitsui Kozan Chemicals Co. Ltd. Treating water containing coal
US4452688A (en) * 1979-09-04 1984-06-05 Electric Power Research Institute Integrated coal liquefication process
US4244530A (en) * 1979-12-17 1981-01-13 Consolidation Coal Company Integrated coal cleaning and slurry preparation process
DE3000791A1 (de) * 1980-01-11 1981-07-16 Deutsche Babcock Ag, 4200 Oberhausen Nassentascher
US4563196A (en) * 1980-07-03 1986-01-07 Ruhrkohle Aktiengesellschaft Coal charging in a coal gasification installation
JPS588719B2 (ja) * 1981-04-09 1983-02-17 三井造船株式会社 石炭を脱灰造粒して輸送する方法
US4529407A (en) * 1981-06-25 1985-07-16 Pickering Fuel Resources, Inc. Fuel pellets
FR2512053B1 (fr) 1981-08-28 1985-08-02 Armines Procede de transformation de matiere ligneuse d'origine vegetale et matiere d'origine vegetale ligneuse transformee par torrefaction
AT372876B (de) * 1981-11-19 1983-11-25 Oesterr Draukraftwerke Verfahren und vorrichtung zur rauchgasentschwefelung von kohlefeuerungen nach dem trocken- additivverfahren
US4504277A (en) * 1982-04-16 1985-03-12 Atlantic Research Corporation Coal-water fuel slurries and process for making same
US4461624A (en) * 1983-02-28 1984-07-24 Gulf Canada Limited Beneficiation of low-rank coals by immersion in residuum
US4510040A (en) * 1983-11-07 1985-04-09 International Coal Refining Company Coal liquefaction process
US4596650A (en) 1984-03-16 1986-06-24 Lummus Crest, Inc. Liquefaction of sub-bituminous coal
US4547282A (en) 1984-04-30 1985-10-15 Lummus Crest, Inc. Coal liquefaction and hydrogenation
US4562748A (en) * 1984-08-16 1986-01-07 The United States Of America As Represented By The United States Department Of Energy Disc valve for sampling erosive process streams
DE3675502D1 (de) 1985-05-24 1990-12-13 Clerc De Bussy Le Verfahren zum erzeugen von geroestetem holz, auf diese weise hergestelltes produkt und dessen verwendung zum erzeugen von energie.
FR2591611B1 (fr) * 1985-12-18 1988-11-10 Armines Nouveau materiau ligno-cellulosique thermocondense, procede et four pour l'obtenir.
JP2813361B2 (ja) * 1989-03-03 1998-10-22 三菱重工業株式会社 微粉炭燃焼方法
US5035721A (en) * 1989-03-30 1991-07-30 Electric Power Research Institute, Inc. Method for beneficiation of low-rank coal
US5054697A (en) 1990-01-02 1991-10-08 Provost Robert S Removable mill throat and wear ring for pulverizer
US5156686A (en) 1990-11-30 1992-10-20 Union Oil Company Of California Separation of oils from solids
US5234577A (en) * 1990-11-30 1993-08-10 Union Oil Company Of California Separation of oils from solids
US5215596A (en) * 1990-11-30 1993-06-01 Union Oil Company Of California Separation of oils from solids
US5199185A (en) * 1991-06-20 1993-04-06 Western Dry, Inc. Process and equipment for gaseous desiccation of organic particles
DE4129240C2 (de) * 1991-09-03 1995-02-02 Steag Ag Verfahren zum Betreiben eines Kohlekraftwerks
US5213635A (en) * 1991-12-23 1993-05-25 General Electric Company Gamma titanium aluminide rendered castable by low chromium and high niobium additives
US5360553A (en) * 1992-09-17 1994-11-01 Baskis Paul T Process for reforming materials into useful products and apparatus
US5269947A (en) 1992-09-17 1993-12-14 Baskis Paul T Thermal depolymerizing reforming process and apparatus
US5387267A (en) * 1993-08-25 1995-02-07 Modular Energy Corporation Process and apparatus for treating heterogeneous waste to provide a homogeneous fuel
DE4446401C2 (de) * 1993-12-27 1998-07-02 Kobe Steel Ltd Fester Brennstoff, hergestellt aus poröser Kohle und Verfahren und Vorrichtung zu dessen Herstellung
JP3008768B2 (ja) * 1994-01-11 2000-02-14 松下電器産業株式会社 バンプの形成方法
US5458786A (en) 1994-04-18 1995-10-17 The Center For Innovative Technology Method for dewatering fine coal
US5601692A (en) * 1995-12-01 1997-02-11 Tek-Kol Partnership Process for treating noncaking coal to form passivated char
US6162265A (en) 1997-03-03 2000-12-19 Fuels Management, Inc. Process for processing coal
ID20131A (id) * 1997-03-31 1998-10-08 Mitsubishi Heavy Ind Ltd Metode dan peralatan pengeringan batu bara, metode untuk penyimpanan lama batu bara yang direformasi dan batu bara yang direformasi yang disimpan lama, dan proses dan sistem untuk produksi batu bara yang direformasi
US6146432A (en) 1999-07-15 2000-11-14 The United States Of America As Represented By The Department Of Energy Pressure gradient passivation of carbonaceous material normally susceptible to spontaneous combustion
US20030221363A1 (en) 2002-05-21 2003-12-04 Reed Thomas B. Process and apparatus for making a densified torrefied fuel
DE102005038135B3 (de) 2005-08-11 2007-03-08 Schottdorf, Bernd, Dr. Vorrichtung und Verfahren zur kontinuierlichen Herstellung von Holzkohle
NL1030864C2 (nl) * 2006-01-06 2007-07-09 Stichting Energie Werkwijze en inrichting voor het behandelen van biomassa.
DK2027233T3 (en) 2006-06-14 2016-01-18 Torr Coal Technology B V Process for the preparation of solid fuels by roasting (torrefaction) as well as that achieved solid fuel and use of this fuel
US20090007484A1 (en) * 2007-02-23 2009-01-08 Smith David G Apparatus and process for converting biomass feed materials into reusable carbonaceous and hydrocarbon products
US8449631B2 (en) 2007-03-18 2013-05-28 John A. Paoluccio Method and apparatus for biomass torrefaction using conduction heating
AU2009231575B2 (en) 2008-04-03 2012-09-27 North Carolina State University Autothermal and mobile torrefaction devices

Patent Citations (64)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3424573A (en) 1964-11-02 1969-01-28 Rocco Catoggio De Villiers Process for combined oxygen iron refining and producing of ferrous melts
US3687431A (en) 1970-12-18 1972-08-29 Aluminum Co Of America Preheating of dry aggregate for carbon electrodes
US4071151A (en) 1976-11-24 1978-01-31 The United States Of America As Represented By The United States Department Of Energy Vibratory high pressure coal feeder having a helical ramp
US4149228A (en) 1977-07-22 1979-04-10 The United States Of America As Represented By The Secretary Of The Army Compact uniform light diffuser and attenuator
US4140228A (en) 1977-12-01 1979-02-20 The United States Of America As Represented By The United States Department Of Energy Dry piston coal feeder
US4142868A (en) 1978-05-02 1979-03-06 The United States Of America As Represented By The United States Department Of Energy Wear compensating seal means for rotary piston coal feeder
US4282006A (en) 1978-11-02 1981-08-04 Alfred University Research Foundation Inc. Coal-water slurry and method for its preparation
US4300291A (en) 1979-03-13 1981-11-17 Salem Corporation Methods and apparatus for heating particulate material
US4486894A (en) 1979-08-07 1984-12-04 Coal Industry (Patents) Limited Method of and apparatus for sensing the ash content of coal
US4341530A (en) 1979-12-05 1982-07-27 The United States Of America As Represented By The Department Of Energy Slurry atomizer for a coal-feeder and dryer used to provide coal at gasifier pressure
US4324544A (en) 1980-06-12 1982-04-13 Fmc Corporation Process and system for drying coal in a fluidized bed by partial combustion
US4353427A (en) 1980-09-26 1982-10-12 Stock Equipment Company Weight-sensor calibration for gravimetric coal feeder
US4470878A (en) 1981-05-13 1984-09-11 Krupp-Koppers Gmbh Method for drying coal and cooling coke
US4606793A (en) 1981-06-11 1986-08-19 Vladan Petrovic Method for the operation of a carbonization plant
US4497122A (en) 1982-02-25 1985-02-05 Fuller Company Rotary coal feeder and dryer
US4468232A (en) 1982-05-05 1984-08-28 Alfred University Research Foundation, Inc. Process for preparing a clean coal-water slurry
US4444129A (en) 1982-11-05 1984-04-24 Lecorp Method of drying fine coal particles
US4430963A (en) 1982-12-03 1984-02-14 General Signal System for generating dry coal weight signal for coal feeder and control system based thereon
US4495710A (en) 1983-08-01 1985-01-29 Atlantic Richfield Company Method for stabilizing particulate low rank coal in a fluidized bed
US4571174A (en) 1984-03-29 1986-02-18 Atlantic Richfield Company Method for drying particulate law rank coal in a fluidized bed
US4575418A (en) 1984-10-03 1986-03-11 The Dow Chemical Company Coal cleaning and the removal of ash from coal
US4617744A (en) 1985-12-24 1986-10-21 Shell Oil Company Elongated slot dryer for wet particulate material
US4852384A (en) 1986-04-21 1989-08-01 The Babcock & Wilcox Company Automatic calibration and control system for a combined oxygen and combustibles analyzer
US4795037A (en) 1986-05-07 1989-01-03 Rich Jr John W Process for separating high ash coal from refuse
US5103743A (en) 1987-09-21 1992-04-14 A. Ahlstrom Corporation Method and apparatus for drying solid material
US5087269A (en) 1989-04-03 1992-02-11 Western Research Institute Inclined fluidized bed system for drying fine coal
US5030054A (en) 1989-06-23 1991-07-09 Detroit Stoker Company Combination mechanical/pneumatic coal feeder
US5050310A (en) 1989-10-13 1991-09-24 Jiles Stephen L Plastic-pipe ovality gauge
US5033208A (en) 1989-12-13 1991-07-23 Kabushiki Kaisha Matsui Seisakusho Hopper dryer
US5171474A (en) 1990-01-22 1992-12-15 Kasei Optonix, Ltd. Method for treating a phosphor
US5174799A (en) 1990-04-06 1992-12-29 Foster Wheeler Energy Corporation Horizontal cyclone separator for a fluidized bed reactor
US5562884A (en) 1990-04-17 1996-10-08 A. Ahlstrom Corporation Reducing N2 O emissions when burning nitrogen-containing fuels in fluidized bed reactors
US5145489A (en) 1990-11-28 1992-09-08 Fuels Management Inc. Method for coprocessing coal and oil
US5327717A (en) 1991-02-05 1994-07-12 Deutsch-Voest-Alpine Industrieanlagenbau Gmbh Process for drying coal for melt-down or coal gasifiers
US5197398A (en) 1991-04-16 1993-03-30 Electric Power Research Institute Separation of pyrite from coal in a fluidized bed
US5625119A (en) 1992-06-22 1997-04-29 Successful Venture Enterprises Inc. Method for treating sludge and soil contaminated with hydrocarbons
US5477850A (en) 1992-10-06 1995-12-26 Rockwell International Corp. Integrated buoyancy suit crew protection system with +/-GZ protection
US5322530A (en) * 1992-10-20 1994-06-21 Western Research Institute Process for clean-burning fuel from low-rank coal
US5411560A (en) 1992-11-05 1995-05-02 Swinburne Limited Method of producing binderless pellets from low rank coal
US5361513A (en) 1992-11-25 1994-11-08 Amax Coal Industries, Inc. Method and apparatus for drying and briquetting coal
US5396260A (en) 1992-12-22 1995-03-07 The Center For Innovative Technology Video instrumentation for the analysis of mineral content in ores and coal
US5265774A (en) 1992-12-29 1993-11-30 Combustion Engineering, Inc. Coal feeder with quick release cleanout door
US5547549A (en) 1993-04-22 1996-08-20 Fraas; Arthur P. Vibrating bed coal pyrolysis system
US5444733A (en) 1993-05-17 1995-08-22 Danieli & C. Officine Meccaniche Spa Electric arc furnace with alternative sources of energy and operating method for such electric furnace
US5534137A (en) 1993-05-28 1996-07-09 Reilly Industries, Inc. Process for de-ashing coal tar
US5546875A (en) 1993-08-27 1996-08-20 Energy And Environmental Research Center Foundation Controlled spontaneous reactor system
US5527365A (en) 1993-11-26 1996-06-18 National Research Council Of Canada Irreversible drying of carbonaceous fuels
US5442919A (en) 1993-12-27 1995-08-22 Combustion Engineering, Inc. Reheater protection in a circulating fluidized bed steam generator
US5568896A (en) 1994-02-22 1996-10-29 Beloit Technologies, Inc. Methods for preparing pulpwood for digestion
US5537941A (en) 1994-04-28 1996-07-23 Foster Wheeler Energy Corporation Pressurized fluidized bed combustion system and method with integral recycle heat exchanger
US5637336A (en) 1994-04-29 1997-06-10 Kannenberg; James R. Process for drying malt
US5471955A (en) 1994-05-02 1995-12-05 Foster Wheeler Energy Corporation Fluidized bed combustion system having a heat exchanger in the upper furnace
US5462932A (en) 1994-05-17 1995-10-31 Merck & Co., Inc. Oral liquid alendronate formulations
US5503646A (en) 1994-06-30 1996-04-02 Fording Coal Limited Process for coal - heavy oil upgrading
US5521132A (en) 1994-09-01 1996-05-28 The United States Of America As Represented By The Secretary Of The Navy Ash-based ceramic materials
US5832848A (en) 1994-10-03 1998-11-10 Quality Heat Treatment Pty, Ltd. Fluidized bed heat treatment furnace
US5730775A (en) * 1994-12-16 1998-03-24 Midrex International B.V. Rotterdam, Zurich Branch Method for rapid reduction of iron oxide in a rotary hearth furnace
US5612003A (en) 1995-10-18 1997-03-18 Fisher-Klosterman, Inc. Fluidized bed wtih cyclone
US5830247A (en) 1997-03-03 1998-11-03 Fuels Management, Inc. Process for processing coal
US5830246A (en) 1997-03-03 1998-11-03 Fuels Management, Inc. Process for processing coal
US5858035A (en) 1997-03-03 1999-01-12 Fuels Management, Inc. Process for processing coal
US5904741A (en) 1997-03-03 1999-05-18 Fuels Management, Inc. Process for processing coal
US20050188608A1 (en) 2001-10-10 2005-09-01 Dunlop Donald D. Process for drying coal
US20060096167A1 (en) * 2001-10-10 2006-05-11 Dunlop Donald D Process for in-situ passivation of partially-dried coal

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
"Chemistry of Coal Utilization", 1963, JOHN WILEY AND SONS, INC.
See also references of EP2480641A4

Also Published As

Publication number Publication date
AU2010298284A1 (en) 2012-05-17
EP2480641A4 (fr) 2013-08-21
AU2010298284B2 (en) 2016-07-07
CA2780314A1 (fr) 2011-03-31
US8197561B2 (en) 2012-06-12
US20100263269A1 (en) 2010-10-21
EP2480641A1 (fr) 2012-08-01

Similar Documents

Publication Publication Date Title
AU2010298284B2 (en) Process for drying coal
US20110314728A1 (en) Method of Simultaneously Drying Coal and Torrefying Biomass
US7695535B2 (en) Process for in-situ passivation of partially-dried coal
US5046265A (en) Method and system for reducing the moisture content of sub-bituminous coals and the like
US5087269A (en) Inclined fluidized bed system for drying fine coal
US4324544A (en) Process and system for drying coal in a fluidized bed by partial combustion
Osman et al. Drying of low-rank coal (LRC)—a review of recent patents and innovations
US20110252698A1 (en) Method of Drying Biomass
US4401436A (en) Process for cooling particulate coal
CN101294765B (zh) 低阶煤高温烟气干燥的方法及装置
US3985516A (en) Coal drying and passivation process
US5904741A (en) Process for processing coal
US20120272569A1 (en) Process for Drying Coal
US6162265A (en) Process for processing coal
US20120023813A1 (en) Method of drying biomass
WO2006044264A2 (fr) Appareil de thermotraitement de matieres particulaires
US5830247A (en) Process for processing coal
US5858035A (en) Process for processing coal
KR20180064561A (ko) 분쇄 및 건조 플랜트
US5830246A (en) Process for processing coal
US20180127671A1 (en) Method of drying biomass
US4325311A (en) Method and equipment for treatment of fuel for fluidized bed combustion
US3896557A (en) Process for drying and stabilizing coal
US7537622B2 (en) Process for drying coal
US4501551A (en) Method for producing a dried particulate coal fuel from a particulate low rank coal

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 10819441

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 2010298284

Country of ref document: AU

Ref document number: 2010819441

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 2780314

Country of ref document: CA

ENP Entry into the national phase

Ref document number: 2010298284

Country of ref document: AU

Date of ref document: 20100923

Kind code of ref document: A